Wastewater treatment apparatus to achieve class b biosolids using chlorine dioxide

ABSTRACT

Disclosed herein are systems and processes for treating a Waste Stream comprising biosolids, the Waste Stream provided at varying flow rates and solids concentrations so as to achieve an SOUR of 1.5 mg O 2 /g/hr or less and an ORP of at least +300 mV. The system includes a biosolids manipulation device to adjust the volume of suspended solids as a percent of the total volume of the Waste Stream to five (5) percent or less; a chemical oxidant feed device to dose the Waste Stream with an oxidant such as chlorine dioxide, ozone, or similar oxidant, and a treatment vessel associated with said chemical oxidant feed device through which said Waste Stream flows, wherein said chemical oxidant feed device and said treatment device are configured so as to achieve a dose rate between 25 and 200 parts per million of the Waste Stream and substantially complete mixing of the oxidant within 30 seconds of dose delivery in the treatment vessel.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is division under 35 U.S.C. § 121 of U.S. patentapplication Ser. No. 13/643,663, titled WASTEWATER TREATMENT APPARATUSTO ACHIEVE CLASS B BIOSOLIDS USING CHLORINE DIOXIDE, filed Dec. 3, 2012,which is a U.S. national stage application and claims the benefit under35 U.S.C. § 371 of PCT/US2011/034116, titled WASTEWATER TREATMENTAPPARATUS TO ACHIEVE CLASS B BIOSOLIDS USING CHLORINE DIOXIDE, filedApr. 27, 2011, which claims priority to U.S. Provisional ApplicationSer. No. 61/328,363, titled WASTEWATER TREATMENT APPARATUS TO ACHIEVECLASS B BIOSOLIDS USING CHLORINE DIOXIDE, filed Apr. 27, 2010, whichpatent applications are hereby incorporated herein by reference in theirentireties for all purposes.

FIELD

This invention relates to wastewater, and more specifically to a meansof wastewater treatment.

BACKGROUND

Certain processes involved in wastewater treatment produce highviscosity slurries, or sludges, and low suspended solid effluents (eacha “Waste Stream”). After treatment, the Waste Stream may be deposited inlandfills, used for certain agricultural purposes or returned to thesurrounding environment. In the U.S., Federal regulations mandate thetreatment of these Waste Streams in order to remove achieve specificstandards. Two specific methods for measuring the degree of treatment ofWaste Streams are the Specific Oxygen Uptake Rate (“SOUR”) and theOxidation Reduction Potential (“ORP”). Conventional techniques do notprovide a cost effective and timely solution for treatment of WasteStreams to specific SOUR and ORP standards. Consequently, there is aneed in the wastewater treatment industry and other industries treatingWaste Streams to more efficiently achieve these specific results.

SUMMARY

The inventors have discovered that the efficiency of the administrationof chemical oxidants such as chlorine dioxide for treating biosolids ina wastewater sample increases dramatically when the percentage ofbiosolids is less than 5 percent and when the chemical oxidant israpidly dispersed in the sample. For example, they have found that largebatch treatments where chemical oxidants are mixed in a batch wastewatersample over the course of a minute had much lower oxygen/reductionpotential, as well as lower disinfection efficiency than the same samplein which the same amount of chemical oxidant that is added on a flow perportion continuous basis. it was unexpected that addition on a flow perportion continuous basis such that rapid dispersal of chemical oxidantis achieved, dramatically increased disinfection efficiency As usedherein, the term “rapid dispersal” or “rapidly disperse” are usedinterchangeably and refer to the substantially uniform dispersal ofchemical oxidant in the Waste Stream within 30 seconds or less, 20seconds or less, 10 seconds or less, or 5 seconds or less.

Not to be bound by any mechanistic theory, it is the inventors beliefthat by providing for the rapid dispersal of the chemical oxidant in awaste stream, versus administration of chemical oxidant in a batchsystem, prevents the unnecessary degradation of the oxidation potentialof the chemical oxidant at only a portion of a sample before thechemical oxidant is sufficiently mixed in the sample. It is believedthat the oxidizing potential is unnecessarily used up on organicmaterials at a portion of the sample whereby oxidation of targetmicrobes is diminished. According to another embodiment, chemicaloxidant is added to the Waste Stream such that the dispersal rate of thechemical oxidant is higher than the degradation rate of the chemicaloxidant.

In one embodiment, the invention pertains to a treatment apparatus toreduce oxygen uptake levels and to increase the ORP of the waste streamis disclosed, consisting of: 1) the mechanical manipulation of thecharacteristics of the Waste Stream to achieve a specific proportion ofconcentration of dissolved and suspended solids to liquid, 2) an oxidantfeed system (utilizing chlorine dioxide, ozone, or similar oxidant) todose the Waste Stream with a dose rate between 25 and 200 parts permillion (“PPM”) of the Waste Stream, and 3) a treatment vessel ofvolumetric dimensions proportional to the flow rate of the Waste Stream.The embodiment of this invention comprises a combination of features andadvantages intended to address various shortcomings conventional WasteStream treatment systems in achieving standards of SOUR and ORP.

The Wastewater Treatment Process

The wastewater treatment process consists of a number of sequentialsteps.

Screening and Primary Treatment

Typically, wastewater enters a wastewater treatment plant at theheadworks. The headworks acts as a primary grit and foreign matterremoval system for a wastewater treatment plant. From the headworkswastewater is transferred to a form of biological treatment unit (“BTU”)(i.e. an oxidation ditch, sequential batch reactor, member bioreactor,etc.). In the BTU Nutrients are removed from the wastewater.

Nitrogen and Phosphorous (“Nutrient”) Removal

The removal of nitrogen is effected through the biological oxidation ofnitrogen from ammonia (nitrification) to nitrate, followed by thereduction of nitrate to nitrogen gas (denitrification). Nitrogen gas isreleased to the atmosphere and thus removed from the water.

Nitrification itself is a two-step aerobic process, each stepfacilitated by a different type of bacteria. The oxidation of ammonia(NH₃) to nitrite (NO₂ ⁻) is most often facilitated by Nitrosomonas spp.(nitroso referring to the formation of a nitroso functional group).Nitrite oxidation to nitrate (NO₃ ⁻), though traditionally believed tobe facilitated by Nitrobacter spp. (nitro referring the formation of anitro functional group), is now known to be facilitated in theenvironment almost exclusively by Nitrospira spp.

Denitrification requires anoxic conditions to encourage the appropriatebiological communities to form. It is facilitated by a wide diversity ofbacteria. Sand filters, lagooning and reed beds can all be used toreduce nitrogen, but the activated sludge process (if designed well) cando the job the most easily. Since denitrification is the reduction ofnitrate to dinitrogen gas, an electron donor is needed. This can be,depending on the wastewater, organic matter (from faeces), sulfide, oran added donor like methanol. Many sewage treatment plants use axialflow pumps to transfer the nitrified mixed liquor from the aeration zoneto the anoxic zone for denitrification. These pumps are often referredto as Internal Mixed Liquor Recycle pumps (IMLR pumps).

Phosphorus removal is important as it is a limiting nutrient for algaegrowth in many fresh water systems. It is also particularly importantfor water reuse systems where high phosphorus concentrations may lead tofouling of downstream equipment such as reverse osmosis filters.

Phosphorus can be removed biologically in a process called enhancedbiological phosphorus removal. In this process, specific bacteria,called polyphosphate accumulating organisms (PAOs), are selectivelyenriched and accumulate large quantities of phosphorus within theircells (up to 20% of their mass). When the biomass enriched in thesebacteria is separated from the treated water, these Biosolids have ahigh fertilizer value.

Phosphorus removal can also be achieved by chemical precipitation,usually with salts of iron (e.g. ferric chloride), aluminum (e.g. alum),or lime. This may lead to excessive sludge productions as hydroxidesprecipitates and the added chemicals can be expensive. Chemicalphosphorus removal requires significantly smaller equipment footprintthan biological removal, is easier to operate and is often more reliablethan biological phosphorus removal.

After treatment to remove Nutrients, the wastewater and accumulatedorganic matter is sent to a clarification process. Clarification iswhere the Waste Streams of wastewater treatment are separated andtypically go to some type of conventional treatment such as aerobic oranaerobic digestion to reduce the biological demand for oxygen andachieve specific standards for oxygen uptake, as demonstrated by theSOUR test.

According to another embodiment, the invention pertains to a wastewatertreatment system that includes a headworks for receiving raw sewagewastewater having biosolids and a biological treatment station that isin fluid communication with said headworks. The system also includes aclarifier in fluid communication with the headworks for concentratingbiosolids from the raw sewage wastewater. In a typical embodiment, theclarifier is in fluid communication with and downstream of thebiological treatment station. Once the raw sewage wastewater has beensubjected to biological treatment and clarification, the biosolid sampleis considered to be waste activated sludge (WAS). Concurrent with orsubsequent to the clarification process, WAS is produced in a wastewaterstream and the amount of biosolids is controlled. Typically, the WAS isadjusted to contain anywhere from 0.5 to 5 percent biosolids, eitherweight/volume (w/v) or by weight (weight percent) depending what isindicated. In a specific embodiment, the biosolid content of the WAS is1-3 percent. The system also includes a first conduit for transportingWAS away from the clarifier. The oxidant addition is associated with thefirst conduit so as to deliver a predetermined dosage of chlorinedioxide, or other oxidant (e.g. to the WAS in the first conduit) at atreatment zone.

Specific Oxygen Uptake Rate (SOUR)

The Specific Oxygen Uptake Rate (SOUR), also known as the oxygenconsumption or respiration rate, is defined as the milligram of oxygenconsumed per gram of volatile suspended solids (VSS) per hour. Thisquick test has many advantages; rapid measure of influent organic loadand biodegradability, indication of the presence of toxic or inhibitorywastes, degree of stability and condition of a sample, and calculationof oxygen demand rates at various points in the aeration basin.

The test was originally developed as a plant control parameter. SOUR isnow also used as an alternative test method to meet the vectorattraction reduction requirement imposed by 40 CFR Part 503 standardsfor the use or disposal of sewage sludge. This requirement reduces thepotential of spreading infectious disease agents by vectors (e.g.insects, rodents, and birds). SOUR-503 is defined as milligram of oxygenconsumed per gram of total solids (TS) per hour. The SOUR test issuitable for solids less than 2% total solids concentration and is usedas an indicator of oxygen demand, similar to a test for BiologicalOxygen Demand, and is not meant to limit the solids concentration of thetarget waste stream.

Oxidation Reduction Potential (ORP)

Oxidation Reduction potential (also known as redox potential,oxidation/reduction potential or ORP) is a measure of the tendency of achemical species to acquire electrons and thereby be reduced. ORP ismeasured in volts (V) or millivolts (mV). Each species has its ownintrinsic reduction potential; the more positive the potential, thegreater the species' affinity for electrons and tendency to be reduced.

Parts Per Million (PPM)

Parts per million is a way of expressing very dilute concentrations ofsubstances. Just as percent means out of a hundred, so parts per millionor ppm means out of a million. Usually describes the concentration ofsomething in water or soil. One ppm is equivalent to 1 milligram ofsomething per liter of water (mg/l) or 1 milligram of something perkilogram soil (mg/kg).

CT

When the biocidal effect of disinfectants are considered, the majorconsiderations are the disinfectant concentration, and the time neededto inactivate exposed organisms. This is generally expressed by theformula: k=C^(n)×t, where C=the disinfectant concentration (mg/L), n=thecoefficient of dilution, t=time (minutes) required to inactivate aspecified percentage of microorganism, and k=a constant for a specificmicroorganism exposed to the disinfectant under specified conditions.

Chemical disinfection can be considered to have the characteristics of afirst-order chemical reaction (Chick's Law), in actual practice, this israrely observed, even in disinfection of drinking water. Other modelshave been applied to disinfection kinetics to account for thesedeviations (Hom Model), but these typically do not account for decay ofor demand on a disinfectant or oxidant.

Although it is standard practice in the field to utilize an oxidant inthe treatment of a waste sample to elevate the oxidation/reductionpotential and effect disinfection of the waste sample, the inventorshave discovered that the degree at which certain oxidants, such aschlorine dioxide, react with the material in the waste stream and arereduced requires the almost instantaneous addition of the oxidant andcomplete mixing in a short period of time. In one embodiment, thepresent invention provides for the addition of sufficient concentrationsof oxidant and mixing with a waste stream so that all of the materialcomes in contact with the oxidant within 10-200 seconds, and all secondintegers there between. This method produces substantially differentresults than other methods in which oxidant addition and mixing takesplace over a period as short as 3 minutes. In an even more specificembodiment, the material comes in contact with the chemical oxidant in30 seconds or less, or 20 seconds or less, or 10 seconds or less or 5seconds or less.

According to another embodiment, the invention pertains to a wastewatertreatment system that includes a headworks for receiving raw sewagewastewater having biosolids and a biological treatment station that isin fluid communication with said headworks. The system also includes aclarifier in fluid communication with the headworks for concentratingbiosolids from the raw sewage wastewater. In a typical embodiment, theclarifier is in fluid communication with and downstream of thebiological treatment station. Once the raw sewage wastewater has beensubjected to biological treatment and clarification, the biosolid sampleis considered to be waste activated sludge (“WAS”). Typically, the WAScontains anywhere from 0.5 to 5 percent biosolids. In a specificembodiment, the biosolid content of the WAS is 1-3 percent. The systemalso includes a first conduit for transporting WAS away from theclarifier. The oxidant addition is associated with the first conduit soas to deliver a predetermined dosage of chlorine dioxide, or otheroxidant (e.g. ozone) to the WAS in the first conduit. The system isequipped with a chemical oxidant source associated with the conduit soas to deliver a predetermined dosage of chemical oxidant. Followingchemical oxidant treatment, the WAS is considered to be a treatedbiosolid sample which meet Class B biosolid standards as defined by theU.S. 40 CFR Part 503. Optionally, the system also includes a dewateringdevice (e.g., a belt filter press or centrifuge device) in fluidcommunication with the first conduit for further removing water from thetreated biosolid sample. Moreover, the system optionally includes asecond conduit for transporting the concentrated treated biosolid samplefrom the dewatering device.

Alternatively, depending on the configuration of a particular wastewatertreatment facility, the process can be used to treat digested sludge,i.e., sludge that has been treated in an anaerobic or aerobic digester,to produce Class B biosolids. In a specific embodiment, primarywastewater, i.e., wastewater not subjected to biological treatment, istransported directly to a digester to produce digested sludge. Thedigested sludge is then subjected to an oxidant treatment zone.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a schematic of a wastewater treatment system that utilizesa chlorine dioxide generating device in a waste activated sludge conduitfor purposes of producing Class B biosolids.

DETAILED DESCRIPTION OF ILLUSTRATED EMBODIMENTS

Disclosed embodiments in this Disclosure are described with reference tothe attached FIGURES, wherein like reference numerals are usedthroughout the FIGURES to designate similar or equivalent elements. Thefigures are not drawn to scale and they are provided merely toillustrate the disclosed embodiments. Several aspects are describedbelow with reference to example applications for illustration. It shouldbe understood that numerous specific details, relationships, and methodsare set forth to provide a full understanding of the disclosedembodiments. One having ordinary skill in the relevant art, however,will readily recognize that the subject matter disclosed herein can bepracticed without one or more of the specific details or with othermethods. In other instances, well-known structures or operations are notshown in detail to avoid obscuring structures or operations that are notwell-known. This Disclosure is not limited by the illustrated orderingof acts or events, as some acts may occur in different orders and/orconcurrently with other acts or events. Furthermore, not all illustratedacts or events are required to implement a methodology in accordancewith this Disclosure.

Notwithstanding that the numerical ranges and parameters setting forththe broad scope of this Disclosure are approximations, the numericalvalues set forth in the specific examples are reported as precisely aspossible. Any numerical value, however, inherently contains certainerrors necessarily resulting from the standard deviation found in theirrespective testing measurements. Moreover, all ranges disclosed hereinare to be understood to encompass any and all sub-ranges subsumedtherein.

A specific example of a wastewater treatment system for producing aClass B Biosolid sample is shown in FIG. 1. In this specific example,wastewater 108 first enters the headworks 110 and then is transferred toa biological treatment station 115. The biological treatment station 115functions primarily to remove biosolid-dissociated nutrients (and a lowpercentage of biosolid-associated nutrients) in the wastewater toproduce a nutrient-reduced wastewater sample 116. The nutrient-reducedwastewater sample 116 is transferred to a clarifier 120, where thenutrient-reduced wastewater sample 116 is separated into an effluentcomponent 121 and a WAS component 122. The effluent component 121 iseither returned to the headworks 110 or is discarded.

According to scheme I., the WAS component 122 is transported in aconduit 124 and subjected to a oxidant treatment zone 125 that is fed byan on-site oxidant generator 127 in fluid communication with the oxidanttreatment zone 125. The biosolids content of the WAS 122 is between 0.5to 5 percent solids. The conduit 124 includes an oxidant administrationcomponent 143, which may be integrated or separate to the conduit,wherein the chemical oxidant is administered to the WAS in a controlledmanner. In particular, the component 143 is configured and associatedwith the oxidant generator 127 such that the chemical oxidant isadministered to WAS to achieve dispersal of the chemical oxidant in theWAS within 30 seconds or less, 20 seconds or less, 15 seconds or less,10 seconds or less, 5 seconds or less, or 2 seconds or less.

Following, oxidant treatment, the WAS 122 is transported to a dewateringdevice 140 (such as a belt filter press or centrifuge device) where morewater is removed from the WAS to achieve a concentrated biosolids sample141 having 12-30 percent biosolids. The, concentrated biosolids sampleachieved prior to the dewatering station 140 has a higher ORP and lowerSOUR.

According to an alternative embodiment, scheme II, raw wastewater isdelivered to a digester 184, either prior or after biological treatment.The raw wastewater is treated in the digester 184 to produce digestedsludge 192. The digested sludge may have 0.5 to 5 percent biosolids. Aconduit 164 transports digested sludge 192 away from the digester 184.The conduit 164 includes a oxidant treatment zone 155. An oxidantgenerator 157 deliver the predetermined dosages to the oxidant treatmentzone 155 at the mixing component 163. The mixing component 163 isconfigured similar to component 143 as discussed above. The digestedsludge 192 is transported to a dewatering device 140, where furtherwater is removed to obtain a concentrated biosolids sample 141 that maybe classified as Class A or Class B biosolids.

While various disclosed embodiments have been described above, it shouldbe understood that they have been presented by way of example only, andnot limitation. Numerous changes to the subject matter disclosed hereincan be made in accordance with this Disclosure without departing fromthe spirit or scope of this Disclosure. In addition, while a particularfeature may have been disclosed with respect to only one of severalimplementations, such feature may be combined with one or more otherfeatures of the other implementations as may be desired and advantageousfor any given or particular application.

Thus, the breadth and scope of the subject matter provided in thisDisclosure should not be limited by any of the above explicitlydescribed embodiments. Rather, the scope of this Disclosure should bedefined in accordance with the following claims and their equivalents.

The terminology used herein is for the purpose of describing particularembodiments only and is not intended to be limiting. As used herein, thesingular forms “a,” “an,” and “the” are intended to include the pluralforms as well, unless the context clearly indicates otherwise.Furthermore, to the extent that the terms “including,” “includes,”“having,” “has,” “with,” or variants thereof are used in either thedetailed description and/or the claims, such terms are intended to beinclusive in a manner similar to the term “comprising.”

Unless otherwise defined, all terms (including technical and scientificterms) used herein have the same meaning as commonly understood by oneof ordinary skill in the art to which embodiments belong. It will befurther understood that terms, such as those defined in commonly useddictionaries, should be interpreted as having a meaning that isconsistent with their meaning in the context of the relevant art andwill not be interpreted in an idealized or overly formal sense unlessexpressly so defined herein.

The disclosure of any cited reference, including related applications,is incorporated herein in its entirety to the extent not inconsistentwith the teachings herein.

1. A system for treating a waste stream comprising biosolids so as toachieve a SOUR of 1.5 mg O2/g/hr or less and an ORP of at least +300 mV,the waste stream being provided at varying flow rates and solidsconcentrations, the system comprising: a biosolids manipulation deviceto adjust the volume of suspended solids as a percent of the totalvolume of the waste stream to five (5) percent or less; a chemicaloxidant feed device to dose the waste stream with a chemical oxidant,and a treatment vessel associated with said chemical oxidant feed devicethrough which said waste stream flows, wherein said chemical oxidantfeed device and said treatment device are configured so as to achieve adose rate between 25 and 200 parts per million of the waste stream andsubstantially complete mixing of the oxidant within 30 seconds of dosedelivery in the treatment vessel.
 2. The system of claim 1, whereinvolumetric dimensions of said treatment vessel and said dose rate issuch to achieve substantially complete mixing of the oxidant within 10seconds.
 3. The system of claim 1, wherein said chemical oxidant ischlorine dioxide, ozone, and combination thereof.
 4. The system of claim3, wherein said chemical oxidant is chlorine dioxide.
 5. A wastewatertreatment system comprising: a headworks for receiving raw sewagewastewater having biosolids; a biological treatment station that is influid communication with said headworks; a clarifier in fluidcommunication with the headworks for concentrating biosolids from theraw sewage wastewater, wherein upon being subject to the biologicaltreatment station and clarifier, the wastewater is converted to wasteactivated sludge (WAS) having a targeted biosolids content; a firstconduit for transporting WAS away from the clarifier comprising atreatment zone; and a chemical oxidant feed device in fluidcommunication with said first conduit so as to dose chemical oxidant andsaid treatment zone, wherein upon being subjected to the treatment zonethe WAS is converted into a treated biosolid sample; wherein saidtargeted bio solids content is 05.-5 percent, w/v, of the WAS.
 6. Thesystem of claim 5, wherein said targeted biosolids content is 1-3percent, w/v.
 7. The system of claim 5, wherein the clarifier isdownstream of the biological treatment station.
 8. The system of claim5, further comprising a dewatering device in fluid communication withthe first conduit for further removing water from the treated biosolidsample.
 9. The system of claim 8, further comprising a second conduitfor transporting the concentrated treated biosolid sample from thedewatering device.
 10. A method of treating primary wastewater toproduce Class B biosolids, the method comprising subjecting the primarywastewater to anaerobic or aerobic digestion to produce digested sludge;and subjecting the digested sludge to dosing of chemical oxidant in atreatment vessel having a treatment zone through which the digestedsludge flows, wherein the dosing achieves a dose rate between 25 and 200parts per million of the digested sludge in the treatment zone andsubstantially complete mixing of the oxidant within 30 seconds of dosedelivery in the treatment vessel. between 25 and 200 parts per millionof the digested sludge in the treatment zone and substantially completemixing of the oxidant within 30 seconds of dose delivery in thetreatment vessel; wherein the primary wastewater is not subjected tobiological treatment prior to becoming digested sludge.
 11. The methodof claim 10, wherein the digested sludge comprises a biosolids contentof 0.5-5 percent, w/v, when in the treatment zone.